Multiphase flow measurement system

ABSTRACT

An automatic well test system ( 100 ) utilizes a two phase vortex separator  104  connected to a pair of Coriolis flowmeters ( 154, 166 ) to measure volumetric flow rates in three phase flow. Measurements are performed according to a process (P 200 ) including an iterative convergence technique. Measurements are enhanced by the use of real time density and water-cut measurements from a water-cut meter ( 172 ) and a water density meter.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention pertains to the field of flow metering technology including systems for use in measuring production volumes including a multiphase mixture of discrete phases, e.g., a mixture including oil, gas, and water phases. More specifically, the separator system utilizes a Coriolis flowmeter in combination with a two phase separator to measure production volumes of the respective components or phases of the multiphase mixture.

2. Statement of the Problem

It is often the case that a fluid flowing through a tubular member contains a plurality of phases, i.e., the fluid is a multiphase fluid. As used herein, the term “phase” refers to a type of fluid that may exist in contact with other fluids, e.g., a mixture of oil and water includes a discrete oil phase and a discrete water phase. Similarly, a mixture of oil, gas, and water includes a discrete gas phase and a discrete liquid phase with the liquid phase including an oil phase and a water phase. The term “fluid” is used herein in the context that fluid includes gas and liquids.

Special problems arise when one uses a flowmeter to measure volumetric or mass flow rates in the combined multiphase flow stream. Specifically, the flowmeter is designed to provide a direct measurement of the combined flow stream, but this measurement cannot be directly resolved into individual measurements of the respective phases. This problem is particularly acute in the petroleum industry where producing oil and gas wells provide a multiphase flow stream including unprocessed oil, gas, and saltwater. Commercial markets exist only for the hydrocarbon products.

It is a common practice in the petroleum industry to install equipment that is used to separate respective oil, gas, and water phases of flow from oil and gas wells. The producing wells in a field or a portion of a field often share a production facility for this purpose, including a main production separator, a well test separator, pipeline transportation access, saltwater disposal wells, and safety control features. Proper management of producing oil or gas fields demands knowledge of the respective volumes of oil, gas and water that are produced from the fields and individual wells in the fields. This knowledge is used to improve the producing efficiency of the field, as well as in allocating ownership of revenues from commercial sales of bulk production.

Early installations of separation equipment have included the installation of large and bulky vessel-type separation devices. These devices have a horizontal or vertical oblong pressure vessel together with internal valve and weir assemblies. Industry terminology refers to a ‘two-phase’ separator as one that is used to separate a gas phase from a liquid phase including oil and water. The use of a two phase separator does not permit direct volumetric measurements to be obtained from segregated oil and water components under actual producing conditions because the combined oil and water fractions are, in practice, not broken out from the combined liquid stream. A ‘three-phase’ separator is used to separate the gas from the liquid phases and also separates the liquid phase into oil and water phases. As compared to two-phase separators, three-phase separators require additional valve and weir assemblies, and typically have larger volumes to permit longer residence times of produced materials for gravity separation of the production materials into their respective oil, gas, and water components.

Older pressure vessel separators are bulky and occupy a relatively large surface area. This surface area is very limited and quite expensive to provide in certain installations including offshore production platforms and subsea completion templates. Some development efforts have attempted to provide multiphase measurement capabilities in compact packages for use in locations where surface area is limited. These packages typically require the use of nuclear technology to obtain multiphase flow measurements.

Coriolis flowmeters are mass flowmeters that can also be operated as vibrating tube densitometers. The density of each phase may be used to convert the mass flow rate for a particular phase into a volumetric measurement. Numerous difficulties exist in using a Coriolis flowmeter to identify the respective mass percentages of oil, gas, and water in a total combined flow stream.

U.S. Pat. No. 5,029,482 teaches the use of empirically-derived correlations that are obtained by flowing combined gas and liquid flow streams having known mass percentages of the respective gas and liquid components through a Coriolis meter. The empirically-derived correlations are then used to calculate the percentage of gas and the percentage of liquid in a combined gas and liquid flow stream of unknown gas and liquid percentages based upon a direct Coriolis measurement of the total mass flow rate. The composition of the fluid mixture from the well can change with time based upon pressure, volume, and temperature phenomena as pressure in the reservoir depletes and, consequently, there is a continuing need to reverify the density value.

U.S. Pat. No. 4,773,257 teaches that a water fraction of a total oil and water flow stream may be calculated by adjusting the measured total mass flow rate for water content, and that the corresponding mass flow rates of the respective oil and water phases may be converted into volumetric values by dividing the mass flow rate for the respective phases by the density of the respective phases. The density of the respective phases must be determined from actual laboratory measurements. The '257 patent relies upon separation equipment to accomplish separation of gas from the total liquids, and this separation is assumed to be complete.

U.S. Pat. No. 5,654,502 describes a self-calibrating Coriolis flowmeter that uses a separator to obtain respective oil and water density measurements, as opposed to laboratory density measurements. The oil density measurements are corrected for water content, which is measured by a water cut monitor or probe. The '502 patent relies upon a separator to eliminate gas from the fluids traveling through the meter, and does not teach a mechanism for providing multiphase flow measurements when gas is part of the flow stream that is applied to the Coriolis flowmeter.

Even three phase separation equipment does not necessarily provide complete separation of the oil phase from the water phase. Water cut probes are used to measure water content in the segregated oil phase because a residual water content of up to about ten percent typically remains in the visibly segregated oil component. The term ‘water cut’ is used to describe the water content of a multiphase mixture, and is most often applied to a ratio that represents a relationship between a volume of oil and a volume of water in an oil and water mixture. According to the most conventional usage of the term ‘water-cut’, well production fluids would have a 95% water-cut when water comprises 95 out of a total 100 barrels of oil and water liquids. The term ‘water-cut’ is sometimes also used to indicate a ratio of the total volume of oil produced to the total volume of water produced. A term ‘oil-cut’ could imply the oil volume divided by the combined oil and water volume. As defined herein, the term ‘water-cut’ encompasses any value that is mathematically equivalent to a value representing water or oil as a percentage of a total liquid mixture including water and oil.

There remains a need to provide a compact package for performing multiphase flow measurements when gas is part of the flow stream and where the package does not require the use of nuclear technology to perform direct measurements on the fluid. Accordingly, it is an aspect of the present invention to provide method and apparatus that is capable of performing multiphase flow measurements in systems having mixtures of gas and liquids or in liquid systems having mixtures of liquids, whether these mixtures are miscible or immiscible.

SOLUTION

The present invention overcomes the problems that are outlined above by providing a fully automated Coriolis-based well test system which does not require manual sampling or laboratory analysis of the production fluids in order to determine the density of the oil and gas components. Additionally, the test system eliminates volumetric measurement errors that derive from the liberation of solution gas at reduced pressures.

The well test system of the invention has two modes of operation. The test system operates as a normal well test system to measure the volume of respective components that are separated from a component mixture, namely, a wellhead production material including oil, gas, and water components. The well test system also has a special density determination mode that avoids the need to obtain hand samples of the production fluids for density measurements. The-on-site density measurements obtained from the system are more accurate than laboratory measurements because the fluids are measured at line conditions.

The system also includes devices that separate a combined flowstream including multiphase wellhead production fluids into separate components. A valve manifold is used to selectively fill a vortex separator with the production of a single well. A gravity separator is used to retain a mixture of oil, gas, and water phases or components from multiple wells while the forces of gravity segregate these components from the production mixture. A dump valve is opened to at least partially drain the liquid components of the production component mixture from the gravity separator after separation of the respective components.

Coriolis flowmeters may be operated in a mass flowmeter mode and densitometer mode. These meters are used to measure the mass flow rates of the respective oil and water components as they leave the respective separators. Density measurements are used obtained from the segregated oil components of multiphase flow. A water-cut monitor is used to obtain water-cut readings of the segregated oil phase. Altogether, fluid density, temperature, mass flow rate, and water-cut measurements are used to calculate a volumetric flow rate for the oil and water components in the production stream. This correction results in a more accurate calculation for the volumetric oil flow rate.

In preferred embodiments, volumetric test errors are also minimized by connecting a pressurized gas source to the test separator. The pressurized gas source is used to maintain a substantially constant separator pressure even when the separator dump valve is permitting flow of liquids from within the test separator.

Other salient features, objects, and advantages will be apparent to those skilled in the art upon a reading of the discussion below in combination with the accompanying drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 depicts a schematic layout of an automated well test system according to the present invention;

FIGS. 2A and 2B depict a flow chart diagram governing the operation of the FIG. 1 system;

FIG. 3 is a plot of hypothetical data demonstrating the practical effects of gas damping on the frequency response of flowtubes in a Coriolis flowmeter; and

FIG. 4 is a plot of hypothetical data showing the relationship between drive gain and time for an event where a transient bubble enters a Coriolis flowmeter.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

FIG. 1 depicts a schematic diagram of a compact multiphase flow measurement system 100 for use in the petroleum industry System 100 includes an incoming multiphase flow line 102 that discharges into a vertical two phase vortex separator 104. In turn, the vortex separator 104 discharges gas into an upper gas measurement flow line 106 and discharges liquids into a lower liquid measurement flow line 108. The gas measurement flow line 106 and the liquid measurement flow line 108 recombine into discharge line 110 after flow measurements have been performed. A controller 112 includes a central processor together with associated circuitry for operating the respective components of system 100. The system 100 is mounted on skid structure 114 for portability, and a production manifold 116 supplies multiphase fluids to system 100 from a plurality of oil or gas wells. Discharge flow line 110 leads to a three phase production separator 118 for separation of gas, water and oil phases prior to a point of commercial sale.

The incoming multiphase flow line 102 receives multiphase fluids including oil, gas, and water from production manifold 116 along the direction of arrow 120. A venturi section 122 utilizes the well known Bernouli effect to reduce pressure in the incoming multiphase fluids within flow line 102 at the throat of the venturi. It is preferred that the degree of pressure reduction occurs to a level which approximates the internal working pressure within the liquid Coriolis meter 166. This reduction in pressure liberates or flashes gas from the multiphase fluids within flow line 102. An incline/decline section 124 facilitates gravity segregation in the gas and liquid phases of the multiphase fluids preceding the vortex separator 104. A horizontal discharge element 126 feeds the vortex separator 104.

Vortex separator 104 is depicted in midsectional view to reveal interior working components. Discharge element 126 is operably positioned for tangential discharge into the cylindrical interior separation section of vortex separator 104. This manner of discharge causes a tornado or cyclone effect to occur in a liquid portion 128 of multiphase fluids within vortex separator 104.

The liquid portion 128 is a majority liquid phase including discrete water, oil, and entrained gas phases. Centrifugal forces arising from the cyclone effect cause additional separation of the entrained gas phase from the liquid portion 128, but it is not possible to completely eliminate the entrained gas phase except at relatively low flow rates permitting additional gravity segregation of the entrained gas phase. The liquid portion 128 discharges from vortex separator 104 into the liquid measurement flow line 108. A water trap 130 is installed in the lower portion of vortex separator 104. This trap may be bled to obtain periodic water density measurements, or a water density meter (not depicted in FIG. 1) may be installed in combination with the trap 130 to provide water density information to controller 112.

A gas portion 132 of the multiphase fluids within vortex separator is a majority gas phase including gas together with mists of oil and water. A mist collecting screen 134 is used for partial condensation of the mists, which in condensed form drip back into the liquid portion 128.

Gas portion 132 discharges into the gas measurement flow line 106. Gas measurement flow line 106 includes a pressure transmitter 135 that transmits an absolute pressure reading of pressure within gas measurement flow line 106 to controller 112 on electrical line 136. Pressure transmitter 135 may be purchased commercially, for example, as a Model 2088 pressure transmitter from Rosemount of Eden Prairie, Minn. A tube 138 connects gas measurement line 136 with the bottom of vortex separator 104. Tube 138 contains a hydrostatic gauge 140 coupled with a pressure transmitter 142 for use in transmitting pressure information concerning the hydrostatic head between point 144 within gas measurement flow line 106 and point 146 at the bottom of vortex separator 104. Electrical line 148 connects the pressure transmitter 142 with controller 112, which uses the hydrostatic head data from pressure transmitter 142 to open and close electrically operable throttling valves 150 and 174 for pressure adjustment assuring proper operation of vortex separator 104, i.e., to prevent vortex separator from becoming overfull with gas to the point where gas portion 132 discharges into liquid measurement flow line 108 or to the point where liquid portion 128 discharges into gas measurement flow line 106. Electrical lines 152 and 176 operably connect controller 112 with the throttling valves 150 and 174, which may, for example, be purchased as Model V2001066-ASCO valves from Fisher of Marshall Town, Iowa.

A Coriolis mass flowmeter 154 in gas measurement flow line 106 provides mass flow rate and density measurements on the gas portion 132 of multiphase fluids within gas measurement flow line 106. The Coriolis mass flowmeter 154 is coupled with a flow transmitter 156 for providing signals representing these measurements to controller 112. Coriolis flowmeter 154 is electronically configured for operations including measurements of mass flow rates, densities, and temperatures of materials passing through gas measurement flow line 106. Exemplary forms of Coriolis flowmeter 154 include the ELITE Models CMF300356NU and Model CMF300H551NU, which are available from Micro Motion of Boulder, Colo.

Electrical line 158 operably couples flow transmitter 156 with controller 112 for transmission of these signals. A check valve 160 in gas measurement flow line 106 assures positive flow in the direction of arrow 162, thus preventing intrusion of liquid portion 128 into gas measurement flow line 106.

Liquid measurement flow line 108 contains a static mixer 164, which turbulates the liquid portion 128 within liquid measurement flow line 108 to prevent gravity segregation of the respective oil, water, and entrained gas phases. A Coriolis flowmeter 166 provides mass flow rate and density measurements of liquid portion 128 within liquid measurement flow line 108, and is connected to flow transmitter 168 for transmission of signals representing these measurements on electrical line 170 to controller 112.

A water cut monitor 172 is installed in liquid measurement flow line 108 to measure the water cut in liquid portion 128 within liquid measurement flow line 108. The type of water-cut monitor is selected depending upon how large the water-cut is expected to be in the flow stream. For example, capacitance meters are relatively inexpensive, but other types of meters may be required where the water-cut may exceed about 30% by volume. Capacitance or resistance probes operate on the principle that oil and water have drastically different dielectric constants. These probes lose sensitivity with increasing water content, and provide acceptably accurate water-cut measurements only where the water volume is less than about 20% to 30% of the total flow stream. The upper 30% accuracy limit is far below the level that is observed from many producing wells. For example, the total liquid production volume of an oil well can be 99% water. Capacitance or resistivity based water-cut monitors, therefore, are relegated to determining the water-cut in an oil component that has a relatively low water content.

Commercially available devices that are used to measure water-cut include near infrared sensors, capacitance/inductance sensors, microwave sensors, and radio frequency sensors. Each type of device is associated with operational limits. Thus, a water-cut probe can measure the volumetric percentage of water in a combined oil and water flow stream.

Water cut monitoring devices including microwave devices are capable of detecting water in an amount up to about one hundred percent of the flow mixture, but in environments including three phase flow are subject to interpreting gas content as oil. This interpretation occurs because microwave detection devices operate on the principle that water in the spectrum of interest absorbs sixty times more microwave energy than does crude oil. The absorption calculations assume that no natural gas is present, but natural gas absorbs twice as much microwave radiation than does crude oil. It follows that a microwave water cut detection system could correct the water cut reading by compensating for the fact that gas in the mixture has affected the measurement.

Electrical line 173 operably connects water cut monitor 172 with controller 112. Controller 112 uses an electrically actuated two-way valve 174 to control pressure in liquid measurement line 108 in a manner that assures proper operation of vortex separator 104 in cooperation with valve 150, i.e., valve 174 is opened and closed to prevent gas portion 132 from discharging into liquid measurement flow line 108 and to prevent liquid portion 128 from discharging into gas measurement flow line 106. Electrical line 176 operably connects valve 174 with controller 112. A check valve 178 in liquid measurement flow line 108 assures positive flow in the direction of arrow 180, thus preventing intrusion of gas portion 132 into the liquid measurement flow line 108. The gas measurement flow line 106 meets in a T with liquid measurement flow line 108 to form a common discharge flow line 110 leading to production separator 118.

Controller 112 is an automation system that is used to govern the operation of system 100. On a basic level, controller 100 includes a computer that is programmed with data acquisition and programming software together with driver circuitry and interfaces for operation of remote devices. A preferred form of controller 112 is the Fisher Model ROC364.

The production manifold 116 contains a plurality of electronically operable three way valves, e.g., valves 182 and 184, which each have corresponding production sources, such as an oil well 186 or a gas well 188. A particularly preferred three-way valve for use in this application is the Xomox TUFFLINE 037AX WCB/316 well switching valve with a MATRYX MX200 actuator. The valves are preferably configured to each receive production fluids from a corresponding individual well, but may also receive production from a group of wells. Controller 112 selectively configures these valves by transmitting signals on electrical line 190. The valves are selectively configured to flow multiphase fluids from a well 186 or combinations of wells (e.g. wells 186 and 188) into rail 192 for delivery of fluids into incoming multiphase flow line 102 while other valves are selectively configured to bypass system 100 by flowing through bypass flow line 194.

Production separator 118 is connected to pressure transmitter 195 and an electrical line 196 for transmission of signals to controller 112. Separator 118 is operably connected with a gas sales line, an oil sales line, and a salt water discharge line (not depicted in FIG. 1) in any conventional manner known to those skilled in the art.

Operation of System 100

FIGS. 2A and 2B depict a schematic process diagram of a process P200 representing control logic for use in programming controller 112. These instructions typically reside in an electronic memory or an electronic storage device for access and use by controller 112. Instructions that embody the process P200 can be storied on any machine readable medium for retrieval, interpretation and execution by controller 112 or similar devices that are connected to system 100 in any operable manner.

Process P200 begins with step P202 in which controller 112 determines that it is proper to enter a production test mode. With regard to FIG. 1, this means that controller 112 selectively configures the valves 182 and 184 of production manifold 116 to flow a well or an operator-selected combinations of wells corresponding to production sources 186 and 188 through rail 192 and into incoming multiphase flow line 102. This determination is usually performed on the basis of a time delay, e.g., to test each well at least once per week. The test mode may also be performed on a continuous basis with the respective valves of production manifold 116 always being selectively configured to flow into system 100 while other valves are configured to bypass system 100 through bypass line 194. These types of well test measurements are conventionally used in allocating, on a deliverability basis, the percentages of the total flow stream that pass through production separator 118 to specific production sources, e.g., sources 186 and 188.

Manually actuated valves 196 and 197 can be opened and closed for selective isolation of system 100, i.e., valves 196 and 197 can both be closed for the removal of all components that are mounted on skid 114. An electrically actuated valve 199 is normally closed. A second or redundant bypass line 198 interior to valves 196 and 197 permits flow to bypass system 100 when valve 199 is open and valves 150 and 174 are closed.

Testing begins in step P204 with controller 112 constricting or opening valves 150 and 174 to reduce or increase the total flow rate through vortex separator 104 for the purpose of separating gas from liquid phases in the multiphase fluid. The total flow rate through system 100 need not be reduced because controller 112 can open valve 199 to permit flow through interior bypass 198. The exact flow rate depends upon the physical volume of the vortex separator and liquid measurement flow line 108, as well as the amount of fluid that sources 186 and 188 are capable of delivering to system 100.

The object of reducing the flow rate through system 100 is to eliminate entrained bubbles from liquid measurement flow line 108 through the use of vortex separator 104 with assistance by gravity segregation while the flow rate is still high enough to prevent substantial gravity segregation of oil from water in the remaining liquid phase. It is also possible to accomplish substantially complete separation of the gas phase from the liquid phase by increasing the flow rate with separation being accomplished by centrifugal forces through vortex separator 104. Controller 112 monitors the drive gain or pickoff voltage from Coriolis flowmeter 166 for this purpose, as explained with reference to FIGS. 3 and 4.

FIG. 3 is a plot of hypothetical data demonstrating the practical effects of gas damping on the frequency response of flowtubes in the Coriolis flowmeter 166 (see also FIG. 1). The log of transmissivity is plotted as a function of the frequency of alternating voltage applied to the drive coil of Coriolis flowmeter 166, e.g., at frequencies f₀, f₁, and f₂. The transmissivity ratio T_(r) equals the output of meter pickoff coils divided by the drive input, i.e., T_(r) is the drive gain: $\begin{matrix} {T_{r} = {\frac{OUTPUT}{INPUT} = \frac{V_{a\quad c}{PICKOFF}\quad {COIL}}{V_{a\quad c}{DRIVE}\quad {COIL}}}} & (1) \end{matrix}$

A first curve 300 corresponds to the undamped system of Equation (1), i.e., no gas is present in the fluid being measured. A second curve 302 corresponds to a damped system where gas is present. Both curves 300 and 302 have an optimal value 304 and 304′, respectively, at the natural frequency f_(n).

FIG. 4 is a plot of hypothetical data showing the relationship between drive gain and time for an event 400 where a transient bubble enters the Coriolis flowmeter 166 as a bubble entrained in a multiphase fluid. The bubble enters at time 402 and exits at time 404. Drive gain is expressed as a percentage in FIG. 4, and plotted as a function of time at intervals, e.g., t₁, t₂, and t₃. Controller 112 (see also FIG. 1) is programmed to monitor drive gain or transmissivity by comparing the same against a threshold value 406. Where the drive gain or transmissivity of curve 408 exceeds threshold 406, controller 112 recognizes that density measurements are affected by the presence of transient bubbles. Thus, Coriolis flowmeter 166 uses only density values obtained when drive gain is less than threshold 406 for purposes of step P206. The exact level of threshold 406 depends upon the specific meter design together with the intended environment of use, and is intended to permit less than one to two percent gas by volume in the multiphase fluid.

In operating Coriolis meters, it is often the case that the pickoff voltage drops in inverse proportion to the event 400 of the curve 408 shown in FIG. 4. The meters are sometimes programmed to sense this drop in amplitude, and they respond by vibrating an oscillation coil to an amplitude of maximum design specification until the gas damping effect is reversed.

With controller 112 opening and/or closing valves 150 and 174 until the drive gain just falls below threshold 406 in the manner described for step P204, step P206 includes Coriolis flowmeter 166 measuring density of the liquid phase without entrained gas. This density measurement is intended to represent density of the liquid phase having no gas voids. This density measurement is referred to as ρ_(L) in the discussion below, and is used to describe the density of a liquid mixture including gas and oil with no entrained gas fraction. As an alternative to performing direct measurements on the multiphase fluid in liquid measurement line 108, it is also possible to obtain samples of the multiphase fluid for laboratory analysis or to approximate density measurements by the use of empirically derived fluid correlations to obtain less preferred approximations of ρ_(L).

In step P208, controller 112 selectively adjusts valves 150 and 174 in a manner that optimizes separation results in vortex separator 104 according to manufacturer's specifications based upon the gross rates of flow through Coriolis flowmeters 154 and 166 together with pressure signals received from pressure transmitter 135 and differential pressure gauge 140. In this step, production manifold 116 is configured to flow for active producing well test measurements. Vortex separator 104 functions differently in this step, as compared to step P204, because controller 112 does not adjust valves 150 and 174 in a manner that reduces drive gain below the threshold 406 shown in FIG. 4. In this circumstance, the majority liquid phase flowing through liquid measurement line 108 may include entrained gas bubbles.

Step P210 includes the use of Coriolis flowmeter 166 to measure the total mass flow rate Q_(TL) of the majority liquid phase including entrained gas within liquid measurement line 108, as well as the density of the majority liquid phase. This density measurement is referred to as ρ_(meas) in the discussion that follows.

In step P212, controller 112 determines the dry gas density ρ_(gas) of the gas in the multiphase fluid. Gas density may be calculated from pressure and temperature information using well known correlations developed by the American Gas Association based upon gas gravity, or laboratory analysis may provide other empirical correlations for gas density determined from actual measurements of produced gas from the multiphase flow stream. Another alternative technique for the determination of gas density is to obtain an actual density measurement from Coriolis flowmeter 154 simultaneously with step P204 or in a separate step P210 where controller 112 selectively adjusts valves 150 and 174 to minimize the drive gain intensity shown in FIG. 4. In some situations, it is also possible to assume that the gas density remains constant because the density of gas is relatively low in comparison to the liquid density, and the assumption of a constant gas density may result in an acceptable level of error.

In step P214, controller 112 calculates a gas void fraction X_(L) in the liquid phase where $\begin{matrix} {{X_{Li} = \frac{\rho_{calc} - {\rho \quad m_{eas}}}{\rho_{calc}}},} & (2) \end{matrix}$

where X_(Li) is the void fraction representing gas void in the multiphase fluid flowing through Coriolis flowmeter 166, i denotes successive iterations, ρ_(meas) is the density measurement obtained in step P210 as described above, and ρ_(calc) is a calculated or estimated density value approximating the density of a multiphase liquid having a void fraction of about X_(Li). Equation (2) will be used in an iterative convergence algorithm. Thus, it is acceptable to begin calculations with a first guess, e.g., a stored value for ρ_(calc) from the preceding cycle of test measurements for a particular production source 186 or an arbitrary value such as 0.8 g/cc.

A particularly preferred manner of providing a first guess for the value of ρ_(calc) is to obtain a water cut measurement from water cut monitor 172. Then, it is possible to assume that no gas is present in the multiphase flow mixture and solve Equation (3) for ρ_(calc):

ρ_(alc) =WC(ρ_(w)−ρ_(o))+ρ_(o)  (3)

where WC is water cut expressed as a fraction comprising the amount of water in the liquid mixture divided by the total volume of the liquid mixture, ρ_(w) is the density of water in the liquid mixture, and ρ_(o) is the density of oil in the liquid mixture. The resultant first guess for ρ_(calc) is the theoretical value of a liquid mixture having no gas void fraction. The measured density ρ_(meas) will be less than ρ_(calc) when x_(i) is greater than zero, provided the values ρ_(w) and ρ_(o) are correct. The values ρ_(w) and ρ_(o) may be obtained from laboratory measurements that are performed on samples of the majority liquid phase including respective oil and water phases. For example, a water density value may be obtained from a hydrometer connected to water trap 130. These values may also be approximated to acceptable levels of accuracy by well known empirical correlations that are published by the American Petroleum Institute.

In step P216, controller 112 performs a calculation to determine whether the last guess for ρ_(calc) has provided a calculation of X_(Li) according to Equation (2) wherein the value of X_(i) has converged within an acceptable range of error. The next guess for ρ_(calc) is calculated as:

ρ_(calci)=(ρ_(gas) X _(Li))+(1−X _(Li))ρ_(L)  (4)

where ρ_(calci) is the next guess for ρ_(calc) calculated using the value X_(Li) from Equation (2), ρ_(L) is the density of the liquid mixture, and the remaining variables are defined above.

Step P218 is a test for convergence wherein convergence exists if the expression:

 D<|ρ _(calci)−ρ_(calc)|  (5)

is true where D is the absolute value of a delimiter representing a negligible error, e.g., 0.01 g/cc, or approximating the limits of precision that is available from Coriolis flowmeter 166, ρ_(calci) is the present value calculated according to Equation (4), and ρ_(calci-1) is the old value of ρ_(calci) from the prior iteration of Equation (2) that produced the X_(Li) value corresponding to ρ_(calci).

Where controller 112 in step P218 determines that there is no convergence, the new guess value ρ_(calci) is substituted for the old guess value ρ_(calc) in step P220, and steps P214 through P218 are repeated until convergence exists.

Water cut may be calculated as: $\begin{matrix} {{WC} = \frac{\rho_{L} - \rho_{O}}{\rho_{W} - \rho_{O}}} & (6) \end{matrix}$

wherein WC is water cut, ρ_(o) is a density of oil in the majority liquid component, and ρ_(w) is a density of water in said majority liquid component. Thus, water cut meter 172 is somewhat redundant if there is no gas phase in the multiphase flow, and may then be optionally eliminated because it is not a required value for this iterative convergence technique.

In step P214A, a more rigorous or noniterative solution is available, provided that the measured water cut value supplied by water cut meter 172 is within a range where the meter functions with acceptable accuracy and precision. The meter reading is a function of the fluid content, and this permits the simultaneous solution of a system of three equations to provide answers for three variables where the equations are:

ρ_(w) q _(w)+ρ_(o) q ₀+ρ_(g) q _(g)=ρ_(mix),  (7)

f(sat)=M  (8)

q _(w) +q ₀ +q _(g)=1  (9)

where ρ_(w) is the density of water in the flow stream, ρ_(o) is the density of oil in the flow stream, ρ_(g) is the density of gas in the flow stream, ρ_(mix) is the density of the combined flow stream, q_(w) is the fractional flow rate of water by volume (i.e., a water-cut), q₀ is the fractional flow rate of oil by volume, q_(g) is the fractional flow rate of gas by volume, and f(sat) is a function of flow stream content that is unique to a particular type of water-cut meter providing a total meter reading M.

Where the water-cut meter is a microwave meter, the function f(sat)=M may be approximated as:

m _(w) q _(w) +m _(o) q _(o) +m _(g) q _(g) =M,  (10)

where m_(w) is the meter reading in pure water, m_(o) is the meter reading in pure oil, m_(g) is the meter reading in pure gas, and the remaining terms are described above. Where, in a typical meter, m_(w)=60, m_(o)=1, and mg=2, Equations (8) through (11) can be solved for q_(w) as: $\begin{matrix} {q_{w} = \frac{\left( {\rho_{mix} - \rho_{o}} \right) - {\left( {M - 1} \right)\left( {\rho_{g} - \rho_{o}} \right)}}{\left( {\rho_{w} - \rho_{o}} \right) - {59\left( {\rho_{g} - \rho_{o}} \right)}}} & (11) \end{matrix}$

where the terms are defined above. Also,

q _(g) =M−1−59q _(w), and  (12)

q _(o)=58q _(w) −M+2.  (13)

Once convergence is achieved in step P218, step P222 entails using Coriolis flowmeter 154 to measure the mass flow rate Q_(TG) and density ρ_(mgas) of the majority gas phase flowing through Coriolis flowmeter 154 under the flow conditions of step P208.

Step P224, as shown in FIG. 2B, includes solving for the gas void fraction X_(G) in the majority gas phase flowing through gas measurement line 106, according to the equation: $\begin{matrix} {{XG} = \frac{P_{mgas} - P_{L}}{P_{gas} - P_{L}}} & (14) \end{matrix}$

where XG is a fraction corresponding to a volume of gas taken with respect to the total volume of the majority gas phase, ρ_(mgas) is a value obtained in step P222, ρ_(gas) is a value obtained in step P212, and ρ_(L) is a value obtained in step P206.

In step P224, the value of water cut obtained from water cut monitor 172 is adjusted, as needed, to compensate for the presence of gas in the majority liquid phase. For example, where the gas void fraction X_(Li) is known, it is possible to use this value to correct water cut readings for microwave absorption based upon the assumption that only oil and water are present.

Step P226 includes using the data thus acquired to solve for the flow rates of the three respective phases in each of the majority liquid phase and the majority gas phase. These equations are useful for this purpose:

Q _(L) =Q _(TL)*(1−X _(i))+Q _(TG)*(1−X _(G));  (15)

Q _(G) =Q _(TL) *X _(i) *Q _(TG) *X _(G);  (16)

Q _(O) =Q _(L)*(1−WC);  (17)

Q _(W) =Q _(L) *WC;  (18)

$\begin{matrix} {{V_{L} = \frac{Q_{L}}{\rho_{L}}};} & (19) \\ {{V_{O} = \frac{Q_{O}}{\rho_{o}}};} & (20) \\ {{V_{G} = \frac{Q_{G}}{P_{gas}}};{and}} & (21) \\ {{V_{W} = \frac{Q_{W}}{P_{W}}},} & (22) \end{matrix}$

wherein Q_(L) is the total mass flow rate of the liquid phases flowing through system 100; Q_(TL) is the total mass flow rate of the majority liquid phase including entrained gas; X_(i) is the gas void fraction in the majority liquid phase determined from step P214 and resulting in convergence in step P218; Q_(TG) is the total gas mass flow rate of the majority gas phase measured in step P222; X_(G) is the gas void fraction in the majority gas phase determined in step P224; Q_(G) is the total gas mass flow rate through system 100; ρ_(O) is the total oil mass flow rate through system 100; Q_(W) is the total water mass flow rate through system 100; WC is the water cut provided from water cut monitor 172 with corrections as needed in step P224; V_(L) is the total volumetric flow rate of the liquid phases flowing through system 100; ρ_(L) is the liquid phase density determined in step P206; V_(O) is the total oil volumetric flow rate through system 100; ρ_(O) is oil density at flow conditions; V_(G) is the total gas volumetric flow rate through system 100; ρ_(gas) is gas density at flow conditions; V_(W) is the total water volumetric flow rate through system 100; and ρ_(W) is water density at flow conditions.

Controller 112 in step P228 provides system outputs including direct temperature, density, and mass flow rate measurements together with calculation results for volumetric and mass flow rates for the respective phases. These flow rates may be integrated over time to provide cumulative production volumes for the test interval.

In step P232, controller 112 determines if a new test configuration should be executed. If controller 112 determines that a new test configuration should be executed, then controller 112 returns to step P204. If controller 112 determines that a new test configuration should not be executed, then controller 112 exits the production test mode in step P234.

Controller 112 in step P230 interacts with system components including production manifold 116 to optimize field efficiency. For example, in an oilfield having drive energy that is predominated by a gas cap, production efficiency is optimized when the gas cap is depleted after the oil is recovered. It is desirable to produce oil referentially before the gas, and the gas-oil contact may move downward into the former oil zone as the oil is depleted. This movement of the gas-oil contact can result in wells that formerly produced primarily oil changing to produce primarily gas. The proper response to this drastically increased gas production in an oil well is normally to shut the well in or reduce its production rate so as not to deplete the drive energy of the reservoir, and controller 112 can be programmed to take this action. Similar responses can be programmed for moving oil-water contacts or even to optimize present economic performance from an accounting standpoint by producing one low cost well before higher cost wells if all other factors are equal.

Those skilled in the art understand that the preferred embodiments described hereinabove may be subjected to apparent modifications without departing from the scope and spirit of the invention. Accordingly, the inventors hereby state their full intention to rely upon the Doctrine of Equivalents in order to protect their full rights in the invention. 

What is claimed is:
 1. A multiphase flow measurement system for use in flow environments including multiple liquid phases and a gas phase comprising: means for separating an incoming multiphase flow into a majority liquid component having a majority liquid content with entrained gas and a majority gas component having a majority gas content; and means for measuring a flow rate of said majority liquid component when said majority liquid component contains entrained gas, wherein said means for measuring a flow rate of said majority liquid component uses a calculation to quantify flowrates of discrete liquid and gas phases in said majority liquid component, said calculation being selected from a group consisting of iterative convergent calculations, rigorous calculations, and combinations thereof.
 2. The multiphase flow measurement system of claim 1 wherein said means for measuring a flow rate of said majority liquid component total includes a mass flowmeter.
 3. The multiphase flow measurement system of claim 2 wherein said mass flowmeter is a Coriolis mass flowmeter.
 4. The multiphase flow measurement system of claim 1 wherein said calculation of said means for measuring a flow rate of said majority liquid component is free of empirically derived correlations except for empirically derived correlations used to determine fluid properties selected from the group consisting of density and viscosity.
 5. The multiphase flow measurement system of claim 4 wherein said means for measuring a flow rate of said majority liquid component includes: means for flowing a first liquid from said separating means in a manner providing essentially no entrained gas bubbles in said first majority liquid; and means for measuring a density ρ_(L) in a first liquid provided by said means for flowing a first liquid when there are essentially no entrained gas bubbles in said first liquid.
 6. The multiphase flow measurement system of claim 5 wherein said means for measuring a flow rate of said majority liquid component includes: means for measuring a density ρ_(meas) in said majority liquid component; and means for calculating a void fraction X_(L) based upon a relationship between a density ρ_(meas) determined by said means for measuring a density ρ_(meas) and a density ρ_(L) determined by said means for measuring a density ρ_(L), and for applying said void fraction X_(L) to a total flow rate Q_(TL) from said means for measuring a total liquid phase flow rate to provide respective flow rates Q_(L) and Q_(G), respectively, corresponding to liquid and gas components of said liquid phase.
 7. The multiphase flow measurement system of claim 6 wherein said means for calculating a void fraction X_(L) includes programmable control logic using an iterative convergence calculation.
 8. The multiphase flow measurement system of claim 7 wherein said iterative convergence calculation converges based upon a difference between a measured density value and a theoretical density value based on the void fraction X_(L).
 9. The multiphase flow measurement system of claim 8 wherein said means for calculating a void fraction X_(L) includes programmable control logic using a noniterative calculation.
 10. The multiphase flow measurement system of claim 9 wherein said means for calculating a void fraction X_(L) includes programmable control logic using means for comparing results from said iterative solution against results from said noniterative calculation.
 11. The multiphase flow measurement system of claim 6 wherein said means for measuring a flow rate of said majority liquid component includes: means for determining a gas density ρ_(gas) at temperature and pressure in said multiphase flow measurement system; means for calculating a density ρ_(calc) based upon a gas density ρ_(gas) from said means for determining a gas density ρ_(gas), in combination with a liquid density ρ_(L) determined by said means for measuring a density ρ_(L), and a void fraction X_(L) determined by said means for calculating a void fraction X_(L).
 12. The multiphase flow measurement system of claim 11 wherein said means for calculating a density ρ_(calc) operates according to a relationship: ρ_(calc)=(P_(gas) X _(L))+(1−X _(L))P _(L), wherein X_(L) is a void fraction of said majority liquid component.
 13. The multiphase flow measurement system of claim 12 wherein said calculation of said means for measuring a flow rate of said majority liquid component is an iterative calculation including means for iterating values of ρ_(calc) through successive values of X_(L) until ρ_(calc) converges within an acceptable range of error with respect to a value ρ_(meas) which is determined by said means for measuring a density ρ_(meas).
 14. The multiphase flow measurement system of claim 13 wherein said means for iterating values of ρ_(calc) operates according to a relationship: X _(Li)=(P _(calc) −P _(meas))/P _(calc), wherein X_(Li) is the gas void fraction based upon an iterative approximation of ρ_(calc).
 15. The multiphase flow measurement system of claim 11 further including means for calculating a water cut WC in said majority liquid phase based upon a density ρ_(calc) determined by said means for calculating a density ρ_(calc) when said second majority liquid phase contains an oil phase and a water phase in an intended environment of use.
 16. The multiphase flow measurement system of claim 15 wherein said means for calculating a water cut operates according to a relationship: WC=(P _(calc) −P _(o))/(P _(w) −P _(o)), wherein WC is water cut, ρ_(o) is a density of oil in said majority liquid component, and ρ_(W) is a density of water in said majority liquid component.
 17. The multiphase flow measurement system of claim 1 including means for measuring a density ρ_(mgas) of a majority gas component delivered from said means for separating an incoming multiphase flow, and for measuring a flow rate of said majority gas component.
 18. The multiphase flow measurement system of claim 17 including means for calculating a void fraction X_(G) in said majority gas phase based upon a density using said density ρ_(mgas) determined from said means for measuring a density ρ_(mgas).
 19. A method of performing multiphase flow measurements in flow environments including a liquid phase and a gas phase, said method comprising the steps of: separating an incoming multiphase flow into a majority liquid component having a majority liquid content with entrained gas and a majority gas component having a majority gas content; and measuring a flow rate of said majority liquid component when said majority liquid component contains entrained gas, wherein said step of measuring a flow rate of said majority liquid component includes calculating to quantify flowrates of discrete liquid and gas phases in said majority liquid component, said step of calculating includes use of a calculation selected from a group consisting of iterative convergent calculations, rigorous calculations, and combinations thereof.
 20. The method of claim 19 wherein said step of measuring a flow rate of said majority liquid component is performed using a mass flowmeter.
 21. The method of claim 20 wherein said mass flowmeter is a Coriolis mass flowmeter.
 22. The method of claim 19 wherein said step of calculating is free of empirically derived correlations except for empirically derived correlations used to determine fluid properties selected from the group consisting of density, viscosity, and no empirically derived correlations.
 23. The method of claim 22 wherein said step of measuring a flowrate of said majority liquid component includes: flowing a first liquid from said separating means in a manner providing essentially no entrained gas bubbles in said first majority liquid; and measuring a density ρ_(L) in a first liquid provided by said means for flowing a first liquid when there are essentially no entrained gas bubbles in said first liquid.
 24. The method of claim 23 wherein said step of measuring a flow rate of said majority liquid component includes: measuring a density ρ_(meas) in said majority liquid component under conditions of normal flow possibly including entrained gas bubbles in said liquid phase; and calculating a void fraction X_(L) based upon a relationship between a density ρ_(meas) determined in said step of measuring a density ρ_(meas) and a density ρ_(L) determined in said step of measuring a density ρ_(L); applying said void fraction X_(L) to a total flow rate Q_(TL) of said majority liquid component to provide respective flow rates Q_(L) and Q_(G), respectively, corresponding to liquid and gas components of said majority liquid component.
 25. The method of claim 24 wherein said step of calculating a void fraction X_(L) includes use of an iterative convergence calculation.
 26. The multiphase flow measurement system of claim 25 wherein said iterative convergence calculation converges based upon a difference between a measured density value and a theoretical density value based on the void fraction X_(L).
 27. The method of claim 26 wherein said step of calculating a void fraction X_(L) includes programmable control logic using a noniterative calculation.
 28. The method of claim 27 wherein said step of calculating a void fraction X_(L) includes comparing results from said iterative solution against results from said noniterative calculation to obtain a best answer.
 29. The method of claim 22 wherein said step of measuring a flow rate of said majority liquid component includes: determining a gas density ρ_(gas) at temperature and pressure in a multiphase flow measurement system; calculating a density ρ_(calc) based upon a gas density ρ_(gas) determined in said step of determining a gas density ρ_(gas), in combination with a liquid density ρ_(L) determined from said step of measuring a density ρ_(L), and a void fraction X_(L) determined from said step of calculating a void fraction X_(L).
 30. The method of claim 29 wherein said step of calculating a density ρ_(calc) operates according to a relationship: P _(calc)=(P _(gas) X _(L))+(1−X _(L))P _(L), wherein X_(L) is a void fraction of said majority liquid component.
 31. The method of claim 30 wherein said step of calculating a density ρ_(calc) is an iterative calculation that includes iterating values of ρ_(calc) through successive values of X_(L) until ρ_(calc) converges within an acceptable range of error with respect to a value ρ_(meas) which is determined from said step of measuring a density ρ_(meas).
 32. The method of claim 31 wherein said step of iterating values of ρ_(calc) operates according to a relationship: X _(Li)=(P _(calc) −P _(meas))/P _(calc), wherein X_(Li) is the gas void fraction based upon an iterative approximation of ρ_(calc).
 33. The method of claim 25 further including a step of calculating a water cut WC in said majority liquid phase based upon a density ρ_(calc) determined from said step of calculating a density ρ_(calc) when said second majority liquid phase contains an oil phase and a water phase in an intended environment of use.
 34. The method of claim 33 wherein said step of calculating a water cut operates according to a relationship: WC=(P _(calc) −P _(o))/(P _(w) −P _(o)), wherein ρ_(o) is a density of oil in said majority liquid component, and ρ_(W) is a density of water in said majority liquid component.
 35. The method of claim 22 including measuring a density ρ_(mgas) of a majority gas component resulting from said step of separating an incoming multiphase flow, and measuring a flow rate of said majority gas component.
 36. The method of claim 35 including a step of calculating a void fraction X_(G) in said majority gas phase based upon a density using said density ρ_(mgas) determined from said means for measuring a density ρ_(mgas). 